US5047299A - Electrochemical cell apparatus having an integrated reformer-mixer nozzle-mixer diffuser - Google Patents

Electrochemical cell apparatus having an integrated reformer-mixer nozzle-mixer diffuser Download PDF

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Publication number
US5047299A
US5047299A US07/559,111 US55911190A US5047299A US 5047299 A US5047299 A US 5047299A US 55911190 A US55911190 A US 55911190A US 5047299 A US5047299 A US 5047299A
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Prior art keywords
mixer
chamber
reforming
fuel
diffuser
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Expired - Fee Related
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US07/559,111
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English (en)
Inventor
Larry A. Shockling
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Westinghouse Electric Corp
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Westinghouse Electric Corp
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Assigned to WESTINGHOUSE ELECTRIC CORPORATION reassignment WESTINGHOUSE ELECTRIC CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: SHOCKLING, LARRY A.
Priority to US07/559,111 priority Critical patent/US5047299A/en
Priority to CA002041718A priority patent/CA2041718A1/en
Priority to NO91912472A priority patent/NO912472L/no
Priority to DE69102106T priority patent/DE69102106D1/de
Priority to EP91306528A priority patent/EP0468699B1/de
Priority to ES91306528T priority patent/ES2053283T3/es
Priority to JP3205548A priority patent/JPH04332476A/ja
Priority to KR1019910012691A priority patent/KR920003573A/ko
Publication of US5047299A publication Critical patent/US5047299A/en
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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/06—Combination of fuel cells with means for production of reactants or for treatment of residues
    • H01M8/0606—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants
    • H01M8/0612—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material
    • H01M8/0625—Combination of fuel cells with means for production of reactants or for treatment of residues with means for production of gaseous reactants from carbon-containing material in a modular combined reactor/fuel cell structure
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/24—Grouping of fuel cells, e.g. stacking of fuel cells
    • H01M8/241—Grouping of fuel cells, e.g. stacking of fuel cells with solid or matrix-supported electrolytes
    • H01M8/2425—High-temperature cells with solid electrolytes
    • H01M8/243—Grouping of unit cells of tubular or cylindrical configuration
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

Definitions

  • This invention relates to a compact, integrated, combination reformer-ejector for an electrochemical apparatus, such as a fuel cell generator, utilizing fresh, gaseous feed fuel which must be reformed.
  • feed fuel either H 2 +CO, or previously reformed natural gas
  • feed fuel is fed into the apparatus at one end and flows parallel to exterior fuel electrode surfaces of the elongated fuel cells.
  • Spent fuel is combusted with spent oxidant in a separate chamber and then exits the apparatus.
  • Natural gas methane plus ethane, propane, butane and nitrogen
  • This natural gas must be reformed, that is, converted to carbon monoxide and hydrogen, through the use of a catalyst and excess water vapor, prior to its utilization in the fuel cell.
  • the reforming reaction is endothermic, requiring a supply of heat, and is best performed at temperatures close to 900° C.
  • the heat required for reforming is a significant fraction of the excess heat that results from fuel cell operation.
  • the use of recirculated spent fuel to provide water vapor and CO 2 for fresh feed fuel, by means of an ejector powered by the inlet fresh fuel pressure, has the potential to result in several problems.
  • the ejector in the typical fuel cell apparatus is located directly in the hot fuel cell environment and is bathed by the hot recirculation gas stream, and the nozzle must be insulated or cooled to prevent carbon deposition from natural gas feed fuel, due to "cracking" which occurs at temperatures above about 400° C.
  • the invention resides in an electrochemical apparatus having a fresh gaseous feed fuel inlet; gaseous feed oxidant inlet; gaseous spent fuel recirculation channel; separate hot combusted exhaust gas exit channel; a generator chamber containing a plurality of electrochemical cells; and a reforming chamber; characterized in that the reforming chamber has a top close to the generator chamber, and a bottom closest to the fresh gaseous feed fuel inlet, and contains: (a) an outer portion containing reforming material, which outer portion connects to the generator chamber, (b) an inner portion containing a mixer-diffuser within a shell barrier, which inner portion connects to the outer portion at the bottom of the reforming chamber, and (c) a middle portion between the inner and outer portions, connected to the gaseous spent fuel recirculation channel at the top of the reforming chamber and feeding into the mixer-diffuser at the bottom of the reforming chamber, where the mixer-diffuser is within the reforming chamber, a mixer nozzle is near the bottom of the reforming
  • the mixer-diffuser has a narrow mixer section which broadens out to a flared diffuser section, so that it has a narrow entrance and a broad exit.
  • the mixer injector which has a narrow opening feeding into the mixer-diffuser forces high pressure feed fuel at a high velocity into the mixer-diffuser, causing aspiration and entrainment of the recirculating spent fuel, the whole, causing an ejector effect.
  • both the mixer nozzle and the mixer diffuser are within the inner portions of the reforming chamber, to provide a compact apparatus.
  • the reforming chamber is readily accessible and removable from the apparatus.
  • the invention also resides in that a portion of the hot combusted exhaust gas exit channel contacts the outside of the reforming chamber, allowing heat transfer between said channel and reforming chamber.
  • the invention further resides in a high temperature electrochemical apparatus, operating on a gaseous oxidant and a fresh gaseous feed fuel, having a fresh gaseous feed fuel inlet; gaseous feed oxidant inlet; gaseous spent fuel recirculation channel; separate hot combusted exhaust gas exit channel; a generator chamber containing a plurality of electrochemical cells; and a reforming chamber; characterized in that the reforming chamber has a top close to the generator chamber, and a cooler bottom close to the fresh gaseous feed fuel inlet, and contains: (a) an outer portion containing reforming material, (b) an inner portion containing a mixer-diffuser, and (c) a middle portion between the inner and outer portions, for receiving hot recirculation gas from the gaseous spent fuel recirculation channel; where the mixer-diffuser is within the reforming chamber, where hot recirculation gas fed into the middle portion of the reforming chamber mixes with fresh gaseous feed fuel at a mixer nozzle near the bottom of the reforming
  • an integrated mixer nozzle and a mixer-diffuser, such as an ejector, within the body of the reforming chamber eliminates complicated crossover gas streams, reduces overall length of the apparatus, makes more efficient use of the reforming material, increases recuperative heat transfer, and reduces the heat loss to the ambient.
  • fuel electrode means that electrode in contact with fuel
  • air electrode means that electrode in contact with air or oxygen
  • spent fuel, oxidant, or air means partially reacted, low BTU fuel or partially reacted, depleted gaseous oxidant, or depleted air containing about 5% to 15% oxygen.
  • spent fuel does not include the mixture of spent fuel combusted with spent oxidant or air, which mixture is herein defined as "combusted exhaust gas”.
  • the location of the mixer-diffuser, and the mixer nozzle in a low-temperature position eliminates the need for forced cooling of the nozzle.
  • the ducts which carry the recirculating spent fuel and which are in contact with the reforming chamber, and the ducts which carry the fuel mixture to and through the reforming material may be concentric, with heat conduction fins providing optimum heat exchange between the two gas streams. This heat exchange minimizes energy loss from the heat capacity of the hot extracted spent fuel, while allowing the nozzle temperature of the ejector, and therefore of the fresh fuel to remain below the 400° C. limit above which carbon deposition has been observed.
  • an electrochemical cell apparatus or generator containing two cell bundles 12 and 14, each bundle containing a plurality of parallel, axially elongated electrochemical cells 16, such as solid oxide fuel cells.
  • the cells are located in generator compartment or section 22.
  • Each cell has an exterior fuel electrode 18 covering its axially elongated surface, shown dotted for the sake of clarity, an interior air electrode, and a solid oxide electrolyte between the electrodes (air electrode and electrolyte not shown), as is well known in the art.
  • the air electrode is generally a doped ceramic of the perovskite family, for example, doped LaMnO 3
  • the electrolyte is generally yttria stabilized zirconia
  • the fuel electrode is generally a zirconia-nickel cermet material.
  • a calcia stabilized zirconia support for the air electrode can also be used.
  • the electrochemical cell apparatus will operate with an interior temperature in the range of about 600° C. to about 1,200° C.
  • An outer housing 20 surrounds the entire apparatus.
  • the housing is preferably comprised of a high temperature resistant metal such as Inconel.
  • Thermal insulation 26, such as low density alumina is contained within the outer housing as shown. Penetrating the housing 20 and insulation 26 is fresh gaseous feed fuel inlet 28, the fresh feed fuel shown as F, and gaseous oxidant, such as air or oxygen, feed 30, as well as ports for electrical leads and the like, not shown.
  • the generator chamber 22 extends between wall 32 and a porous barrier 34.
  • the porous barrier 34 need not be a sealed structure.
  • the porous barrier 34 is designed to allow spent fuel gas flow, indicated by arrows 36, from the generator chamber 22, operating at a pressure slightly above atmospheric, to the combustion chamber 24, operating at a slightly lower pressure, where the spent gas combines with spent oxidant, forming exhaust gas which passes through channel 45.
  • High temperature, elongated, solid oxide electrolyte cells 16 extend between the combustion chamber 24 and the wall 32.
  • the cells have open ends 44 in the combustion chamber 24, and closed ends in the generator chamber 22 near wall 32.
  • Each individual cell generates approximately one volt on open circuit, and a plurality are electrically interconnected through conducting felts 40, usually nickel fiber metal, preferably in a series-parallel rectangular array, as described in U.S. Pat. No. 4,395,468, herein incorporated by reference.
  • a gaseous oxidant such as air
  • oxidant feed inlet 30 enters the oxidant feed conduits 42 at a temperature of approximately 500° C. to 700° C., and a pressure above atmospheric, being optionally heated prior to entering the housing by conventional means, such as a heat exchanger coupled with a blower.
  • the oxidant, within the conduits, is passed through the combustion chamber 24, where it is further heated to a temperature of approximately 800° C. to 900° C. by the combusted exhaust gas.
  • the oxidant then flows through the length of the oxidant circuit, through the conduits 42 which extend down the inside length of the fuel cells, being further heated to approximately 1,000° C., by virtue of absorbing most of the heat generated during the electrochemical reaction. A smaller fraction of the heat is absorbed by the fuel.
  • the oxidant is discharged into the closed end bottom of the fuel cells 16.
  • the oxidant within the fuel cells reverses direction, and electrochemically reacts at the inner air electrode along the inside active length of the cells, depleting somewhat in oxygen content as it approaches the open ends 44 of the cells.
  • the depleted oxidant is then discharged into the combustion chamber 24 through the open cell ends 44, and is shown as spent oxidant streams 35.
  • This spent oxidant combusts with depleted fuel, where part of the total depleted fuel passes through porous barrier 34 as shown by arrows 36, to form combusted exhaust gas 47, which exits the apparatus through combusted exhaust gas exit channels 45, which can be routed to contact the reforming chamber 54, as shown, finally exiting as exhaust gas E.
  • the channels 45 can be made of a high temperature resistant metal, such as Inconel.
  • a gaseous fuel that has not yet been reformed such as a gaseous hydrocarbon, including hydrocarbons such as methane (CH 4 ), ethane (C 2 H 6 ), propane (C 3 H 8 ), and the like, vaporized petroleum fractions such as naphtha, and alcohols, such as ethyl alcohol (C 2 H 5 OH), and the like, and natural gas, typically a mixture of 85% methane and 10% ethane with a balance of propane, butane and nitrogen, can be used.
  • a gaseous hydrocarbon including hydrocarbons such as methane (CH 4 ), ethane (C 2 H 6 ), propane (C 3 H 8 ), and the like
  • vaporized petroleum fractions such as naphtha
  • alcohols such as ethyl alcohol (C 2 H 5 OH)
  • natural gas typically a mixture of 85% methane and 10% ethane with a balance of propane, butane and nitrogen
  • a major portion of the hot gaseous spent fuel formed along the axial length of the cells 16 passes to at least one hot spent fuel recirculation channel 46, which can be made of a high temperature resistant metal such as Inconel.
  • Another portion of the hot spent fuel passes into combustion chamber 24, shown as arrows 36, as previously described, to combust with spent air, shown as arrow 35, and preheat the fresh oxidant feed.
  • the hot spent fuel recirculation channel 46 passes from the generator chamber 22 to feed into the top of the middle portion of the reforming chamber 54 and combine with the fresh feed fuel inlet at the entrance to the mixer chamber 52, at a mixer nozzle 50, at the bottom of the reforming chamber 54.
  • This mixer nozzle 50 is located near the bottom of the reformer chamber at the entrance to the mixer-diffuser chamber 52. This allows recirculation of the portion of the spent fuel fed into channel 46 to mix with the fresh feed fuel near mixer nozzle 50, to provide a reformable fuel mixture of the two gases, shown by arrows 51.
  • the mixer nozzle 50 is preferably within the inner portion of the reforming chamber 54, that is at the bottom of the reforming chamber near the entrance to the mixer-diffuser, where fresh fuel and spent fuel meet, as shown. Unless the mixer nozzle is clearly removed from the reforming chamber it is considered “within” the reforming chamber.
  • the geometry of the mixer nozzle/mixer-diffuser is further designed such that the dynamic energy of the fuel at the nozzle 50 is effectively and efficiently converted to an elevated pressure. This is preferably accomplished by having the cross-sectional area get larger as it proceeds from the mixer-diffuser entrance near nozzle 50, to its exit in one fashion as shown. The spent fuel and fresh fuel mix at the bottom of the mixer-diffuser 52, and are expanded at the top.
  • the reformable fuel mixture 51 will contain at least water vapor (steam) and usually also H 2 , CO, and CO 2 , all contributed by the spent fuel that enters mixer-diffuser chamber 52.
  • the volume ratio of spent fuel to fresh feed fuel will be adjusted by the velocity of the fresh feed fuel input so that approximately 2 volumes to 5 volumes of water vapor and CO 2 are added to each volume of fresh feed fuel, when the fuel, is natural gas.
  • the presence of water vapor plus a reforming catalyst, most commonly Ni, allows conversion of gaseous hydrocarbons to CO+H 2 , by the reaction: ##STR1##
  • the reformable fuel mixture 51 then passes through a series of passageways, from the mixer-diffuser chamber exit into and through an outer portion of reforming chamber 54, containing reforming material 56, such as nickel, or the like, or other well-known useful reforming material for fuel gas.
  • reforming material 56 such as nickel, or the like, or other well-known useful reforming material for fuel gas.
  • the reforming chamber 54 has a top portion 55 closest to the generator chamber 22 and a bottom portion 57 closest to the fresh gaseous feed fuel inlet 28, and has an integrated mixer nozzle 50 and mixer-diffuser 52 contained within its structure.
  • the reforming chamber 54 is preferably of concentric tubular design, with an outer section or channel containing the reforming material 56, and connected with an inner section or channel containing mixer nozzle 50 and mixer-diffuser 52, both contained within shell barrier 61, and a middle section or channel 64 between the inner and outer portions, for receiving hot recirculation gas from the gaseous spent fuel recirculation channel 46.
  • the mixer nozzle 50 and mixer-diffuser 52 are both within the reforming chamber and substantially exterior to the main portion of the apparatus, as shown in the FIGURE. Both the mixer nozzle and mixer diffuser are readily accessible and readily removable from the apparatus.
  • Hot recirculation gas flowing downward in middle section or channel 64 between the outer section and the exterior of shell 61 passes into the bottom of the inner section and mixes with fresh gaseous feed fuel F at the mixer nozzle 50, near the bottom portion 57 of the reforming chamber 54.
  • the recirculation gas in channel 64 transfers heat to the fuel mixture inside shell 61 and to the reforming material 56.
  • the mixture enters the narrow bottom section of mixer-diffuser 52 and expands as it travels upward within the mixer-diffuser 52, as it passes to a top portion of the reforming chamber at the top of shell 61.
  • the expanded mixture then flows back toward the bottom portion 57 of the reforming chamber around the outside of the mixer-diffuser 52, in a channel between the mixer-diffuser and the inside of shell 61, all the while being heated by the hot recirculation gas in the channel 64.
  • the expanded mixture then enters the outer portion or channel of the reforming chamber, which contains reforming material, near the bottom portion 57 of the reforming chamber 54 through inlets 65 and again flows upward through the reforming material 56 in the outer portion of the reforming chamber.
  • This outer portion of the reforming chamber connects to the generator chamber 22, through channels 58 and 59, or any other series of passageways; that is, it is connected in some fashion by passageways.
  • hot recirculation gas flows downward, around the shell 61, then upward within the mixer-diffuser 52, then downward again around the outside of the mixer-diffuser within the shell 61, and finally through inlets 65 into the outer portion containing the reforming material where the mixture again flows upward toward the generator chamber. All the winding gas flow allows enhanced recuperation of heat, and compaction of design so that the entire generator apparatus can be made smaller from top to bottom.
  • Hot spent fuel from channel 46 reaches the entrance to middle section or channel 64 at a temperature of approximately 1,000° C.
  • Section 64 in contact with the outer section of the reforming chamber, allows heat transfer to the reforming material 56. Heat transfer also occurs between section or channel 64 and the downward flow of reformable fuel mixture within shell 61. This reduces the spent fuel temperature, provides heat for the endothermic reforming reaction, and provides preheating of the reformable fuel mixture.
  • complete reforming of the fuel is not necessary since some internal catalytic reforming of the reformable fuel mixture, by the nickel fiber felts 40, or the nickel cermet surface 18 of the fuel cells, within the generator chamber 22, can be utilized to keep the amount of reforming material 56 relatively small.
  • the temperature of the spent fuel drops from approximately 1,000° C. at the entrance to middle section 64, to a sufficiently low temperature as it approaches the nozzle 50 such that the fuel in the mixer-diffuser chamber 52 will not exceed 400° C.
  • the combusted exhaust gas E in separate channels 45 can contact the sides of the reforming chamber 54, and will pass out of the apparatus at approximately 700° C.
  • the entire reforming chamber 54 with integrated mixer nozzle and mixer-diffuser subassembly is essentially interior, but exteriorly bolted onto the electrochemical apparatus 10.
  • the mixer nozzle 50, and mixer-diffuser 52, while part of the electrochemical apparatus are integrated with but substantially spaced apart from the combustion chamber 24 and the generator chamber 22.
  • the mixer nozzle 50 can operate at below approximately 400° C., which would be the approximate temperature at the mixer nozzle 50 and entrance to the mixer-diffuser 52.
  • the mixer nozzle is extended by gaseous component ducts or channels to a position remote from the high-temperature active generating and combusting region of the apparatus, and can operate at a sufficiently low temperature to prevent carbon deposition.
  • the gaseous component ducts or channels are coupled or arranged in a manner to facilitate heat exchange from hot spent fuel to a reformable fuel mixture, thus conserving much of the thermal energy of the recirculating fuel gas, while maintaining a low nozzle temperature to prevent carbon deposition.
  • This combination coupled with reformer contact and double reverse flow of the gases involved, allows utilization of the high temperature spent fuel gas to provide a portion of the endothermic energy requirement of the reforming reaction.
  • the primary gas seals can be extended and located in a colder region 67, and allow ease of disassembly and replacement of the reforming chamber 54 and the integrated mixer nozzle 50, and mixer diffuser 52, as a cartridge unit.

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US07/559,111 1990-07-25 1990-07-25 Electrochemical cell apparatus having an integrated reformer-mixer nozzle-mixer diffuser Expired - Fee Related US5047299A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
US07/559,111 US5047299A (en) 1990-07-25 1990-07-25 Electrochemical cell apparatus having an integrated reformer-mixer nozzle-mixer diffuser
CA002041718A CA2041718A1 (en) 1990-07-25 1991-05-02 Electrochemical cell apparatus having an integrated reformer-mixer nozzle-mixer diffuser
NO91912472A NO912472L (no) 1990-07-25 1991-06-25 Elektrokjemisk celleapparat med integrert reformeringsanlegg -blanderdyse -blanderspreder.
EP91306528A EP0468699B1 (de) 1990-07-25 1991-07-18 Elektrochemische Zellen enthaltender Apparat, bei dem der Reformer, die Mischdüse und der Mischverteiler integriert sind
DE69102106T DE69102106D1 (de) 1990-07-25 1991-07-18 Elektrochemische Zellen enthaltender Apparat, bei dem der Reformer, die Mischdüse und der Mischverteiler integriert sind.
ES91306528T ES2053283T3 (es) 1990-07-25 1991-07-18 Aparato de celulas electroquimicas con conjunto integrado de reformador-tobera mezcladora-difusor mezclador.
JP3205548A JPH04332476A (ja) 1990-07-25 1991-07-22 改質器、混合ノズル、混合拡散器を一体化した電気化学的セル装置
KR1019910012691A KR920003573A (ko) 1990-07-25 1991-07-24 일체형 리포머-믹서 노즐-믹서 디퓨저를 갖는 전기화학 전지장치

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US07/559,111 US5047299A (en) 1990-07-25 1990-07-25 Electrochemical cell apparatus having an integrated reformer-mixer nozzle-mixer diffuser

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US (1) US5047299A (de)
EP (1) EP0468699B1 (de)
JP (1) JPH04332476A (de)
KR (1) KR920003573A (de)
CA (1) CA2041718A1 (de)
DE (1) DE69102106D1 (de)
ES (1) ES2053283T3 (de)
NO (1) NO912472L (de)

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US5527631A (en) * 1994-02-18 1996-06-18 Westinghouse Electric Corporation Hydrocarbon reforming catalyst material and configuration of the same
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US6472092B1 (en) * 1998-08-12 2002-10-29 Honda Giken Kogyo Kabushiki Kaisha Fuel-reforming apparatus comprising a plate-shaped reforming catalyst
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US20030157386A1 (en) * 2002-02-20 2003-08-21 Ion America Corporation Load matched power generation system including a solid oxide fuel cell and a heat pump and an optional turbine
US6610434B1 (en) * 2000-08-10 2003-08-26 Siemens Westinghouse Power Corporation Segregated exhaust SOFC generator with high fuel utilization capability
US6655325B1 (en) 1999-02-01 2003-12-02 Delphi Technologies, Inc. Power generation system and method with exhaust side solid oxide fuel cell
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US7066973B1 (en) 1996-08-26 2006-06-27 Nuvera Fuel Cells Integrated reformer and shift reactor
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JPH04332476A (ja) 1992-11-19
NO912472L (no) 1992-01-27
DE69102106D1 (de) 1994-06-30
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ES2053283T3 (es) 1994-07-16
KR920003573A (ko) 1992-02-29
EP0468699B1 (de) 1994-05-25
EP0468699A1 (de) 1992-01-29

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